US4801443A - Sulphur recovery process - Google Patents
Sulphur recovery process Download PDFInfo
- Publication number
- US4801443A US4801443A US07/047,136 US4713687A US4801443A US 4801443 A US4801443 A US 4801443A US 4713687 A US4713687 A US 4713687A US 4801443 A US4801443 A US 4801443A
- Authority
- US
- United States
- Prior art keywords
- catalyst
- sulphur
- gaseous stream
- regenerator
- continuously
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/02—Preparation of sulfur; Purification
- C01B17/04—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides
- C01B17/0404—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by processes comprising a dry catalytic conversion of hydrogen sulfide-containing gases, e.g. the Claus process
- C01B17/0426—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by processes comprising a dry catalytic conversion of hydrogen sulfide-containing gases, e.g. the Claus process characterised by the catalytic conversion
- C01B17/0443—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by processes comprising a dry catalytic conversion of hydrogen sulfide-containing gases, e.g. the Claus process characterised by the catalytic conversion in a moving bed
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/02—Preparation of sulfur; Purification
- C01B17/04—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides
- C01B17/0404—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by processes comprising a dry catalytic conversion of hydrogen sulfide-containing gases, e.g. the Claus process
- C01B17/0426—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by processes comprising a dry catalytic conversion of hydrogen sulfide-containing gases, e.g. the Claus process characterised by the catalytic conversion
- C01B17/043—Catalytic converters
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
Definitions
- This invention relates to improved sulphur recovery units and to processes which use these units. More particularly, this invention relates to a sulphur recovery process and apparatus which continuously circulates catalyst and which may be operated in a smooth and continuous fashion.
- the present invention is directed to chemical reactions leading to the removal of sulphur compounds from gaseous streams. This removal is generally carried out through the partial oxidation of H 2 S by air, thereby forming a mixture of H 2 S and SO 2 , and through the subsequent reaction of H 2 S and SO 2 to produce elemental sulphur and water vapor.
- H 2 S The partial oxidation of H 2 S is frequently accomplished in Claus reaction furnaces using controlled amounts of air to obtain approximately a 2:1 H 2 S/SO 2 mixture in the resulting gases. Although a substantial part of the subsequent H 2 S and SO 2 reaction also frequently occurs in reaction furnaces, generally up to one-third of the H 2 S and SO 2 present in the reaction furnace must be transferred downstream for further catalytic processing.
- sulphur containing gases removed from the reaction furnaces are typically heated to a temperature above the sulphur dew point in order to avoid plugging the catalyst pores. At such temperatures, the rate of reaction is relatively slow and has to be repeated, generally three times, to achieve up to 98% (theoretical) conversion. In addition, the sulphur vapor produced in this reaction generally must be condensed after each step and reaction gases have to be reheated prior to contacting the next catalyst bed.
- tail gas clean up units operate using catalysts similar to those included in upstream catalyst converters, but at temperatures below the sulphur dew point in order to improve conversion. Catalyst plugging generally occurs in these units, which requires the use of multiple units and thus intermittent operation. Generally, multiple units are utilized such that when catalyst sulphur plugging reaches a predetermined value in one converter, a freshly regenerated converter is engaged in operation while the catalyst in the plugged converter is regenerated. Typically, three converters are used, one in production, one being regenerated, and one in post-regeneration cooling.
- a catalyst regenerator having a gas stream inlet means and a gas stream outlet means and a catalyst inlet means and a catalyst outlet means, and said catalyst regenerator containing a moving bed of catalyst particles;
- an apparatus for sulphur recovery comprises:
- a catalyst regenerator having gas inlet and outlet means, catalyst inlet and outlet means, and at least one gas-solid separator;
- a sulphur condenser having gas inlet and outlet means and sulphur outlet means, and connected to said catalyst regenerator such that a relatively sulphur rich gas outlet stream from the regenerator is received in said sulphur condenser and separated into a sulphur stream and an outlet gas stream containing a reduced quantity of sulphur;
- a catalyst contactor having gas inlet and outlet means and catalyst inlet and outlet means and at least one gas-solid separator
- conduit means for transporting regenerated catalyst from the regenerator through the catalyst outlet means, to the catalyst contactor inlet means and into the catalyst contactor;
- conduit means for transporting said sulphur condenser outlet gas stream to said catalyst contactor gas inlet means and contacting the stream with the catalyst;
- conduit means for transporting catalyst from the outlet of the catalyst contactor to the inlet of the catalyst regenerator.
- FIG. 1 is a schematic drawing of a sulphur recovery unit operated in accordance with a preferred embodiment of the present invention
- FIG. 2 is a schematic drawing of a sulphur recovery unit operated in an alternate preferred embodiment of the present invention
- FIG. 3 is a top view of a multicyclone battery included in the catalyst contactor and catalyst regenerator of FIGS. 1 and 2;
- FIG. 4 is a top view of a single cyclone separator of the type shown in FIG. 3;
- FIG. 5 is a side view of a single cyclone separator shown in FIGS. 3 and 4.
- Sulphur recovery units are a secondary part of a wide range of primary processes, such as the treatment of coal, oil and gas. Accordingly, the particular feed to the sulphur recovery unit can vary. However, this feed will typically contain sulphur compounds in gaseous forms such as H 2 S and/or SO 2 .
- Acid gas stream 10 is mixed with air stream 12 as controlled by an analyzer 14.
- the acid gas is then burned in a reaction furnace 16 and the hot reaction gases pass through a line 18 into a catalyst regenerator 20.
- the hot reaction gas enters the regenerator near the bottom causing fluidization of fine catalyst particles above a mesh screen 22. Concurrently, the hot reaction gas also vaporizes sulphur from the catalyst surface.
- Fine catalyst particles are separated from the sulphur-containing gas in a multicyclone separator battery 24 located near the head of the regenerator 26.
- the dust free rich sulphur gas exits from the regenerator through line 28 and enters sulphur condenser 30.
- any sulphur accumulating in the regenerator 20 may be removed via a drain 31.
- sulphur condenser heat from the sulphur rich gas and condensing sulphur is utilized to produce steam, as indicated by steam line 32 and feed water line 33.
- the condensed sulphur is drained through line 34 and taken to storage.
- Relatively cool reaction gas is removed from the sulphur condenser through line 36 and is further cooled by mixing with a small recycle stream of tail gas 38.
- the mixed gas stream 40 is then further cooled through heat exchange in the air cooler 42, with sour water being removed through line 44.
- the cool recycle gas stream 46 is directed to a recycle gas blower 48 and then to a catalyst ejector 50 where hot regenerated catalyst is blended with the recycle gas stream and carried to the bottom of the catalyst contactor vessel 52.
- a tangential inlet nozzle arrangement causes swirling of the catalyst particles located in contactor 52, thus extending the contacting time between the catalyst and the sulphur containing gases.
- the tail gas leaving the catalyst contactor through line 54 is separated from the catalyst particles by means of a multicyclone battery 56. If desired, fine solids may be removed through a sock filter 58 prior to recovery of the tail gas through line 60. Catalyst is then returned to the catalyst contactor by means of line 62.
- an acid gas stream 110 is mixed with an air stream 112 and passed to an existing Claus furnace 114 for initial removal of sulphur products through line 116.
- An exiting gas stream 118 containing, for example, approximately 10% gaseous sulphur compounds is transferred to a salt bath heater 120 at a rate of approximately 40,000 pounds/hour.
- the gaseous stream 122 is introduced to a catalyst regenerator 124.
- a catalyst regenerator 124 relatively hot acid gas vaporizes sulphur present on the surface of the fine catalyst particles.
- the sulphur rich gas is then separated from the catalyst particles by means of a cyclone separator battery located within the catalyst regenerator.
- a sulphur rich gas stream 126 is removed from catalyst regenerator 124 and passed to a sulphur condenser 128 while regenerated catalyst is removed from the lower section of catalyst regenerator through line 130.
- sulphur condenser 128 sulphur is removed through line 132 at a rate of approximately 5,000 pounds per hour while sulphur condenser outlet gas is removed through line 134 at a rate of approximately 38,000 pounds per hour.
- sulphur condenser outlet gas is passed to a water separator 138.
- sour water is recovered through line 140 and passed to pump 142 for removal from the system while cool recycle gas stream 144 is directed to a compressor 146 at a rate of roughly 29,000 pounds/hour.
- a recycle gas stream 148 is then mixed with regenerated catalyst from line 130 and a resultant stream 150 is introduced to a catalyst contactor 152.
- the resultant relatively sulphur free tail gas is removed through line 154 and passed to a sock filter 156 for removal of fine catalyst particles. If desired, these fine catalyst particles can be combined with recycle gas stream 148 by means of a catalyst make-up pot 158.
- sulphur containing catalyst from the catalyst contactor is passed through a line 160 to catalyst regenerator 124 at a rate of approximately 0.08 cubic feet per second for contact with hot acid gases as described previously.
- the present invention further comprises a unique apparatus for accomplishing sulphur recovery.
- this apparatus comprises catalyst regenerator 124 and inlet and outlet gas and catalyst lines 122, 126, , 130 and 160, sulphur condenser 127 and inlet and outlet lines 126, 132 and 134, gas recycle line 148, catalyst contactor 152, inlet line 150 which may also concurrently function as a lift pipe reactor, and outlet line 154.
- the catalyst regenerator and catalyst contactor each contain gas-solid separation means.
- This gas-solid separation means can be of various configurations, such as one or more filters or electrostatic precipitators.
- these separation means comprise a battery of cyclone separators shown schematically in FIGS. 3, 4 and 5.
- FIG. 3 shows a top view of the multicyclone battery geometry comprising cyclones of the type shown at 24 in FIG. 1.
- the inside diameter 200 of the cyclone separators would be approximately 6 inches with the outside diameter 202 of each cyclone separator being approximately 12 inches.
- the distance 206 from the axial center of the regenerator to the center of each cyclone separator would be approximately 81/2 to 9 inches.
- the above figures are presented for purposes of illustration and do not limit or define the scope of this invention.
- FIG. 4 shows a top view of an individual cyclone shown in FIG. 3 and illustrates a unique spiral arrangement within each cyclone separator.
- each cyclone contains an inner spiral plate 208 designed to increase the curvature of the cyclone contant surface. Since gas-solid cyclone separation is based, in part, on centrifugal force effects, inclusion of the inner spiral plate enhances the overall separation. This is particularly important in separation systems involving catalyst particles of 150 Tyler mesh or smaller.
- the inner spiral plate 208 forms a smooth curved spiral.
- S represents the distance at a given point of the inner surface from the longitudinal center of the cyclone
- D represents the diameter of the cyclone
- deg represents the number of radial degrees from a fixed point where the inner surface meets the outer cyclone surface.
- point 210 would represent 0 degrees
- point 212 would represent 90 degrees
- point 214 would represent 180 degrees
- point 216 would represent 270 degrees
- point 218 would represent 360 degrees.
- each cyclone contains an inlet pipe 220 as shown in FIGS. 1, 4 and 5.
- FIG. 5 shows a partial side view of the cyclone shown in FIG. 4.
- catalyst and gases enter the cyclone through inlet 220 and are swirled through contact with the inner spiral plate, the lower edge 226 of which is of a sinusoidal shape. Gases flow out the top of the cyclone, with catalyst descending through the lower cyclone portion 224.
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
Abstract
Description
______________________________________ Catalyst Designation F-1 S-100 H-151 ______________________________________ Size 1/4" to 8 MESH 1/4" 1/4" 1/2" to 1/4" Shape granular spherical spherical SA,M.sup.2 / 250 325 400 PBD,LBS/FT.sup.3 52 47 51 Abrasion, WT % 1.4 .10 .20 AL.sub.2 O.sub.3, WT % 92.3 94.6 90.4 NA.sub.2 O .60 .35 1.6 FE.sub.2 O.sub.3 .04 .04 .04 SIO.sub.2 .09 .03 2.0 LOI (1200° C.) 7.0 5.0 6.0 100.0 100.0 100.0 ______________________________________
Claims (1)
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CA000509245A CA1307652C (en) | 1986-05-13 | 1986-05-13 | Mte sulphur recovery process |
CA509245 | 1986-05-13 |
Publications (1)
Publication Number | Publication Date |
---|---|
US4801443A true US4801443A (en) | 1989-01-31 |
Family
ID=4133153
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US07/047,136 Expired - Lifetime US4801443A (en) | 1986-05-13 | 1987-05-08 | Sulphur recovery process |
Country Status (2)
Country | Link |
---|---|
US (1) | US4801443A (en) |
CA (1) | CA1307652C (en) |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5055283A (en) * | 1989-12-22 | 1991-10-08 | Degussa Aktiengesellschaft | Method of removing sodium polysulfide from used sodium/sulfur batteries |
WO1995007855A1 (en) * | 1993-09-14 | 1995-03-23 | The Ralph M. Parsons Company Ltd. | Improvements in or relating to sulphur production from sulphur-bearing gas streams |
US20140030171A1 (en) * | 2012-07-27 | 2014-01-30 | Ripi | Nanocatalyst and Process for Removing Sulfur Compounds from Hydrocarbons |
Citations (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US28830A (en) * | 1860-06-26 | Improvement in grain-binders | ||
US3607132A (en) * | 1969-09-05 | 1971-09-21 | Amoco Prod Co | Vertical sulfur recovery plant |
USRE28830E (en) | 1970-05-22 | 1976-05-25 | Amoco Production Company | Method for reducing sulfur compounds in sulfur plant effluent |
US4255408A (en) * | 1977-11-11 | 1981-03-10 | Thermo-Mist Company | Process for removing sulfur and sulfur compounds from the effluent of industrial processes |
US4309402A (en) * | 1977-12-10 | 1982-01-05 | Davy International Ag | Process and apparatus for production of elemental sulfur |
US4479928A (en) * | 1981-08-19 | 1984-10-30 | Societe Nationale Elf Aquitaine (Production) | Catalytic process for the production of sulphur from a gas containing H.sub. S |
US4504459A (en) * | 1983-07-11 | 1985-03-12 | Stothers William R | Extraction of elemental sulphur from sulphur compound gases |
US4526590A (en) * | 1983-05-31 | 1985-07-02 | Standard Oil Company (Indiana) | Cooling and condensing of sulfur and water from Claus process gas |
-
1986
- 1986-05-13 CA CA000509245A patent/CA1307652C/en not_active Expired - Lifetime
-
1987
- 1987-05-08 US US07/047,136 patent/US4801443A/en not_active Expired - Lifetime
Patent Citations (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US28830A (en) * | 1860-06-26 | Improvement in grain-binders | ||
US3607132A (en) * | 1969-09-05 | 1971-09-21 | Amoco Prod Co | Vertical sulfur recovery plant |
USRE28830E (en) | 1970-05-22 | 1976-05-25 | Amoco Production Company | Method for reducing sulfur compounds in sulfur plant effluent |
US4255408A (en) * | 1977-11-11 | 1981-03-10 | Thermo-Mist Company | Process for removing sulfur and sulfur compounds from the effluent of industrial processes |
US4309402A (en) * | 1977-12-10 | 1982-01-05 | Davy International Ag | Process and apparatus for production of elemental sulfur |
US4479928A (en) * | 1981-08-19 | 1984-10-30 | Societe Nationale Elf Aquitaine (Production) | Catalytic process for the production of sulphur from a gas containing H.sub. S |
US4526590A (en) * | 1983-05-31 | 1985-07-02 | Standard Oil Company (Indiana) | Cooling and condensing of sulfur and water from Claus process gas |
US4504459A (en) * | 1983-07-11 | 1985-03-12 | Stothers William R | Extraction of elemental sulphur from sulphur compound gases |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5055283A (en) * | 1989-12-22 | 1991-10-08 | Degussa Aktiengesellschaft | Method of removing sodium polysulfide from used sodium/sulfur batteries |
WO1995007855A1 (en) * | 1993-09-14 | 1995-03-23 | The Ralph M. Parsons Company Ltd. | Improvements in or relating to sulphur production from sulphur-bearing gas streams |
US20140030171A1 (en) * | 2012-07-27 | 2014-01-30 | Ripi | Nanocatalyst and Process for Removing Sulfur Compounds from Hydrocarbons |
Also Published As
Publication number | Publication date |
---|---|
CA1307652C (en) | 1992-09-22 |
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Date | Code | Title | Description |
---|---|---|---|
AS | Assignment |
Owner name: MULTI-TASK ENGINEERING LTD., 9203 MACLEOD TRAIL SO Free format text: ASSIGNMENT OF ASSIGNORS INTEREST.;ASSIGNOR:SIMEK, IRON O.;REEL/FRAME:004743/0363 Effective date: 19870626 Owner name: MULTI-TASK ENGINEERING LTD.,CANADA Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNOR:SIMEK, IRON O.;REEL/FRAME:004743/0363 Effective date: 19870626 |
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Free format text: PATENTED CASE |
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Free format text: REFUND OF EXCESS PAYMENTS PROCESSED (ORIGINAL EVENT CODE: R169); ENTITY STATUS OF PATENT OWNER: SMALL ENTITY |
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FPAY | Fee payment |
Year of fee payment: 4 |
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SULP | Surcharge for late payment | ||
AS | Assignment |
Owner name: SIMEK, IRON OTTO, CANADA Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNOR:MULTITASK ENGINEERING LTD.;REEL/FRAME:006608/0765 Effective date: 19900430 |
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